WO2015115269A1 - Scandium recovery method - Google Patents

Scandium recovery method Download PDF

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WO2015115269A1
WO2015115269A1 PCT/JP2015/051501 JP2015051501W WO2015115269A1 WO 2015115269 A1 WO2015115269 A1 WO 2015115269A1 JP 2015051501 W JP2015051501 W JP 2015051501W WO 2015115269 A1 WO2015115269 A1 WO 2015115269A1
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scandium
step
extraction
organic solvent
solution
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PCT/JP2015/051501
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French (fr)
Japanese (ja)
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達也 檜垣
佳智 尾崎
松本 伸也
いつみ 松岡
秀昌 永井
俊彦 永倉
工藤 敬司
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住友金属鉱山株式会社
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Priority to JP2014016901 priority
Priority to JP2014-065879 priority
Priority to JP2014065879A priority patent/JP5954350B2/en
Application filed by 住友金属鉱山株式会社 filed Critical 住友金属鉱山株式会社
Publication of WO2015115269A1 publication Critical patent/WO2015115269A1/en

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    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B59/00Obtaining rare earth metals
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00Obtaining aluminium
    • C22B21/0015Obtaining aluminium by wet processes
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/0004Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/0005Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds, e.g. acyclic or carbocyclic compounds, heterocyclic compounds, organo- metallic compounds, alcohols, ethers, or the like
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08Sulfuric acid, other sulfurated acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/42Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00Obtaining refractory metals
    • C22B34/30Obtaining chromium, molybdenum or tungsten
    • C22B34/32Obtaining chromium
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/20Process efficiency
    • Y02P10/21Process efficiency by recovering materials
    • Y02P10/212Recovering metals from waste
    • Y02P10/234Recovering metals from waste by hydro metallurgy

Abstract

In order to recover high-quality scandium from nickel oxide ores efficiently, this method comprises: a leaching step (S1) for feeding Ni oxide ores and sulfuric acid into a pressure vessel, and subjecting the mixture to solid-liquid separation to form a leachate and a leach residue; a neutralization step (S2) for adding a neutralizing agent to the leachate, and thus forming a neutralization sediment and a post-neutralization fluid; a sulfurization step (S3) for adding a sulfurizing agent to the post-neutralization fluid, and separating the obtained mixture into Ni sulfide and a post-sulfurization fluid; an ion-exchange step (S4) for bringing the post-sulfurization fluid into contact with a chelating resin, making Sc adsorbed on the chelating resin, and forming an Sc eluate; a solvent extraction step (S6) for bringing the Sc eluate into contact with an extracting agent, adding a back-extraction agent to the extract, and thus forming back-extracted matter; and a roasting step (S8) for roasting the back-extracted matter, and thus forming Sc oxide. It is preferable that the method further includes, after the ion exchange step (S4), a concentration step (S5) for forming a sediment from the Sc eluate and dissolving the sediment in an acid, and includes, after the solvent extraction step (S6), an Sc precipitation step (S7) for dissolving the back-extracted matter in hydrochloric acid, adding oxalic acid to the obtained solution, and thus forming Sc oxalate crystals.

Description

Scandium recovery method

The present invention relates to a method for recovering scandium, more specifically, a method for efficiently recovering scandium contained in nickel oxide ore by using a chelate resin and solvent extraction with an acidic extractant.

Scandium is extremely useful as an additive for high-strength alloys and as an electrode material for fuel cells. However, since the production amount is small and expensive, it has not been widely used.

Incidentally, nickel oxide ores such as laterite or limonite ore contain a small amount of scandium. However, since nickel oxide ore has a low nickel-containing grade, it has not been industrially used as a nickel raw material for a long time. Therefore, there has been little research on industrially recovering scandium from nickel oxide ore.

However, in recent years, an HPAL process in which nickel oxide ore is charged into a pressure vessel together with sulfuric acid and heated to a high temperature of about 240 to 260 ° C. to separate into solid and liquid a leaching solution containing nickel and a leaching residue has been put into practical use. is there. Impurities are separated by adding a neutralizing agent to the leachate obtained by this HPAL process, and then a sulfiding agent is added to recover nickel as nickel sulfide. The nickel sulfide is then recovered in the existing nickel smelting process. Electrical nickel and nickel salt compounds are obtained by treatment.

When using the HPAL process as described above, scandium contained in nickel oxide ore is contained in the leachate together with nickel (see Patent Document 1). When the neutralization agent is added to the leachate obtained by the HPAL process to separate impurities, and then the sulfiding agent is added, nickel is recovered as nickel sulfide, while scandium is acidic after the addition of the sulfiding agent. Since it is contained in the solution, nickel and scandium can be effectively separated by using the HPAL process.

As a method for recovering scandium from the acidic solution, it has been proposed to adsorb scandium to a chelate resin having iminodiacetate as a functional group to separate and concentrate it from impurities (see Patent Documents 2 to 4). .

By the way, a method of recovering scandium from nickel oxide ore using solvent extraction has also been proposed (see Patent Document 5). In Patent Document 5, 2-ethylhexylsulfonic acid-mono-2-ethylhexyl is added to a scandium-containing solution in an aqueous phase containing at least one of iron, aluminum, calcium, yttrium, manganese, chromium, and magnesium in addition to scandium. In order to separate the yttrium, iron, manganese, chromium, magnesium, aluminum, calcium extracted with the scandium component in the organic solvent by adding an organic solvent diluted with kerosene, and then extracted with scandium in the organic solvent, After scrubbing by adding an aqueous hydrochloric acid solution to remove yttrium, iron, manganese, chromium, magnesium, aluminum, and calcium, an aqueous NaOH solution is added to the organic solvent, and the remaining scandium in the organic solvent is Sc (OH) 3. A slurry containing Sc (OH) 3 obtained by filtering this was dissolved in hydrochloric acid to obtain a scandium chloride aqueous solution, and oxalic acid was added thereto to form a scandium oxalate precipitate. The precipitate was filtered, and iron, manganese, chromium, magnesium, It has been proposed to obtain high-purity scandium oxide by separating aluminum and calcium into a filtrate and then calcining.

JP-A-3-173725 JP-A-1-133920 JP-A-9-176756 JP-A-9-194211 JP-A-9-291320

However, if the chelate resin is used alone, the distribution of iron, aluminum, chromium, etc. in the eluent is very small, but since it is contained in a large amount in the raw material, it must be adsorbed multiple times for separation. Elution operation is required. In addition, although the adsorption / elution behavior of a plurality of impurities contained in a very small amount is inferior to that of scandium, it is difficult to separate due to high distribution in the eluent.

On the other hand, in the solvent extraction, since the scandium quality contained in the nickel oxide ore is very small, it is difficult to process the process liquid directly because the recovery rate and equipment capacity increase.

Thus, no method suitable for industrial recovery of scandium from nickel oxide ore was found.

The object of the present invention is to easily and efficiently recover high-quality scandium from nickel oxide ore.

As a result of intensive studies to solve the above problems, the present inventors have obtained a high-quality scandium by roasting scandium-containing materials obtained by separating scandium with a chelate resin and subjecting it to solvent extraction. Has been found to be obtained simply and efficiently, and the present invention has been completed. Specifically, the present invention provides the following.

(1) The present invention is a leaching process in which nickel oxide ore containing scandium, aluminum and chromium is charged together with sulfuric acid into a pressure vessel and separated into a leaching solution and a leaching residue under high temperature and high pressure, A neutralization step of adding a neutralizing agent to obtain a neutralized starch and a post-neutralization solution; a sulfidation step of adding a sulfiding agent to the post-neutralization solution and separating the nickel sulfide and the post-sulfurization solution; The post-sulfurization solution is contacted with a chelate resin to adsorb the scandium to the chelate resin, an ion exchange step for obtaining a scandium eluent, the scandium eluent is brought into contact with an extractant, and a back extractant is added to the extract This is a scandium recovery method comprising a solvent extraction step for obtaining a back extract and a roasting step for firing the back extract to obtain scandium oxide.

(2) Further, in the present invention, the chelate resin is a resin having iminodiacetic acid as a functional group, and the ion exchange step causes the post-sulfurization solution to contact the chelate resin to adsorb the scandium to the chelate resin. An adsorption step, an aluminum removal step of contacting the chelate resin adsorbed with scandium in the adsorption step with 0.1N or less sulfuric acid, and removing the aluminum adsorbed on the chelate resin in the adsorption step, and the aluminum removal step. The obtained chelate resin is contacted with 0.3N or more and less than 3N sulfuric acid to obtain the scandium eluate, and the scandium elution step is contacted with 3N or more sulfuric acid, and the chelate resin is used in the adsorption step. The process according to (1), comprising a chromium removal process for removing chromium adsorbed on the resin. It is an indium recovery method.

(3) Moreover, this invention further includes the concentration process which produces | generates the starch containing scandium from the said scandium eluent after the said ion exchange process, and melt | dissolves this starch to obtain a scandium concentrate. The solvent extraction step is the scandium recovery method according to (1) or (2), including a step of bringing the scandium concentrate into contact with the extractant to obtain a back extract.

(4) Moreover, this invention is a process in which the said concentration process produces | generates a neutralized material by adding a neutralizing agent to the said scandium eluent, and adjusting pH to the range of 8-9, The method for recovering scandium according to (3), comprising a step of acid-dissolving the hydrate with sulfuric acid or hydrochloric acid.

(5) Further, according to the present invention, the concentration step includes the step of forming scandium oxalate crystals by adding oxalic acid to the scandium eluent, and the scandium oxalate crystals are dissolved in sulfuric acid or hydrochloric acid. The scandium recovery method according to (3) or (4).

(6) Further, the present invention is the scandium recovery method according to any one of (1) to (5), wherein the extractant is an acidic extractant.

(7) Further, the present invention is the scandium recovery method according to (6), wherein the acidic extractant is di-2-ethylhexyl phosphoric acid.

(8) Further, in the invention, the back extractant is sodium hydroxide having a concentration of 5 mol / l or more and 8 mol / l or less, and the back extract is a precipitate of scandium hydroxide. (7) The scandium recovery method according to any one of (7).

(9) Moreover, this invention is an extraction process in which the said solvent extraction process mixes the said scandium eluent and the said extractant which is an organic solvent, and isolate | separates into the organic solvent after extraction which extracted the scandium, and an extraction residual liquid. And a hydrochloric acid solution having a concentration of 5.0 mol / l or more and 7.0 mol / l or less or a sulfuric acid solution having a concentration of 2.5 mol / l or more and 3.5 mol / l or less mixed with the organic solvent after extraction. A scrubbing step of separating impurities from the organic solvent after extraction to obtain an organic solvent after washing; and adding the back extractant to the organic solvent after washing, and back-extracting scandium from the organic solvent after washing to produce the back extract The scandium recovery method according to any one of (1) to (8), including a back extraction step of obtaining

(10) Moreover, the present invention is the scandium recovery method according to (9), wherein the acidic extractant is 2-ethylhexylsulfonic acid-mono-2-ethylhexyl.

(11) Moreover, this invention mixes the said scandium eluent and the said extractant which is an organic solvent, and isolate | separates into the organic solvent after extraction which extracted the scandium, and the extraction residual liquid, and the said organic after extraction Impurities from the organic solvent after the extraction by mixing a hydrochloric acid solution having a concentration of 5.0 mol / l to 7.0 mol / l or a sulfuric acid solution having a concentration of 2.0 mol / l to 5.0 mol / l in the solvent. A scrubbing step for separating and washing to obtain an organic solvent, and a step of adding 5 mol / l or more and 8 mol / l or less of sodium hydroxide to the scrubbing organic solvent obtained in the scrubbing step to obtain a scandium hydroxide starch, A method for recovering scandium according to (10), comprising the step of adding an acid to the scandium hydroxide starch to obtain a scandium solution.

(12) Further, the present invention provides a scandium precipitation step in which, after the solvent extraction step, the back extract is dissolved with hydrochloric acid, and oxalic acid is added to a hydrochloric acid solution obtained by the dissolution to obtain scandium oxalate crystals. The scandium recovery method according to any one of (1) to (9), wherein the roasting step includes a step of firing the scandium oxalate crystals.

According to the present invention, high-quality scandium can be efficiently recovered from nickel oxide ore.

It is a figure for demonstrating the collection method of the scandium which concerns on this invention. It is a figure which shows the extraction rate of Sc, Th, U, Al, and Fe which are contained in an organic solvent when the said collection | recovery method is used. It is a figure which shows the relationship between a sulfuric acid concentration when using the said collection | recovery method, and a washing | cleaning rate.

Hereinafter, specific embodiments of the present invention will be described in detail. However, the present invention is not limited to the following embodiments, and may be implemented with appropriate modifications within the scope of the object of the present invention. Can do.

FIG. 1 is a view for explaining a scandium recovery method according to the present invention. The present invention includes a leaching step S1 in which nickel oxide ore containing scandium, aluminum and chromium is charged into a pressure vessel together with sulfuric acid and separated into a leaching solution and a leaching residue under high temperature and high pressure, and the leaching solution is neutralized. A neutralizing step S2 for adding an agent to obtain a neutralized starch and a post-neutralized solution; a sulfurizing step S3 for adding a sulfiding agent to the post-neutralized solution and separating the nickel sulfide and the post-sulfurized solution; The post-sulfurization solution is brought into contact with a chelate resin to adsorb the scandium to the chelate resin, an ion exchange step S4 for obtaining a scandium eluate, the scandium eluent is brought into contact with an extractant, and a back extractant is added to the extract Thus, a scandium recovery method comprising: a solvent extraction step S6 for obtaining a back extract and a roasting step S8 for firing the back extract to obtain scandium oxide.

The present invention is characterized in that ion exchange and solvent extraction are used in combination in recovering and purifying scandium. By using the method of the present invention, impurities can be separated with higher quality, and stable operation can be performed with compact equipment even from a raw material containing many impurities such as nickel oxide ore.

Although not an essential aspect, after the ion exchange step S4 and prior to the solvent extraction step S6, a scandium-containing starch is produced from the scandium eluent, and this starch is acid-dissolved to obtain a scandium concentrate. You may perform concentration process S5.

In addition, although not an essential aspect, after the solvent extraction step S6, prior to the roasting step S8, the back extract is dissolved with hydrochloric acid, and oxalic acid is added to the hydrochloric acid solution obtained by this dissolution to obtain scandium oxalate. The scandium precipitation step S7 for obtaining crystals may be further performed.

Although not an essential aspect, a neutralizing agent is added to the scandium eluent obtained in the ion exchange step S4 (step S101), then a reducing agent is added (step S102), and then sulfuric acid is added (step S103). ) To obtain a solution after the pH adjustment of the scandium eluent, and the ion exchange step S4 may be performed again using this solution after the pH adjustment. By passing through these steps, the quality of the recovered scandium can be further enhanced.

<Leaching step S1>
In the leaching step S1, nickel oxide ore containing scandium, aluminum, and chromium is charged into a pressure vessel together with sulfuric acid, and is solid-liquid separated into a leachate and a leach residue under high temperature and pressure.

The leaching step S1 may be performed according to a conventionally known HPAL process, and is described in Patent Document 1, for example.

<Neutralization step S2>
In the neutralization step S2, a neutralizing agent is added to the leachate obtained in the leaching step S1 to obtain a neutralized starch and a neutralized solution. Valuable metals such as scandium and nickel are contained in the solution after neutralization, and most of impurities such as aluminum are contained in the neutralized starch.

A conventionally known neutralizing agent is sufficient, and examples thereof include calcium carbonate, slaked lime, and sodium hydroxide.

In the neutralization step, the pH is preferably adjusted in the range of 1 to 4, and more preferably in the range of 1.5 to 2.5. A pH of less than 1 is not preferable because neutralization is insufficient and the neutralized starch and the post-neutralized solution may not be separated. If the pH exceeds 4, not only impurities such as aluminum but also valuable metals such as scandium and nickel are included in the neutralized starch, which is not preferable.

<Sulfurization step S3>
In the sulfiding step S3, a sulfiding agent is added to the neutralized solution to separate the sulfide and the sulfidized solution. Nickel, cobalt, zinc and the like are contained in the sulfide, and scandium and the like are contained in the post-sulfurized solution.

The sulfurizing agent may be any conventionally known one, and examples thereof include hydrogen sulfide gas, sodium sulfide, sodium hydrogen sulfide and the like.

<Ion exchange step S4>
In the ion exchange step S4, the solution after sulfurization is brought into contact with the chelate resin to adsorb scandium to the chelate resin, thereby obtaining a scandium eluent. Although the aspect of the ion exchange step S4 is not particularly limited, the ion exchange step S4 includes an adsorption step S41 in which the sulfidized solution is brought into contact with the chelate resin to adsorb scandium to the chelate resin, and the adsorption step S41. Sulfuric acid of 0.1N or less is brought into contact with the chelate resin adsorbing scandium, and an aluminum removal step S42 for removing aluminum adsorbed on the chelate resin in the adsorption step S41, and 0.3N or more in the chelate resin that has undergone this aluminum removal step S42 3N or less, more preferably 0.4N or more and 0.6N or less sulfuric acid is contacted, and a scandium elution step S43 to obtain a scandium eluent, and a chelate resin that has undergone this scandium elution step S43 is contacted with 3N or more sulfuric acid. Chromium for removing chromium adsorbed on chelate resin in step S41 Preferably includes a removed by step S44.

[Adsorption process S41]
In the adsorption step S41, the sulfidized solution is brought into contact with the chelate resin to adsorb scandium to the chelate resin.

The type of chelate resin is not particularly limited, but is preferably a resin having iminodiacetic acid as a functional group.

Incidentally, the lower the pH range, the smaller the amount of impurities contained in the nickel oxide ore. Therefore, the adsorption | suction to the chelate resin of an impurity can be suppressed by letting the liquid of the pH range as low as possible flow through a chelate resin. However, when the pH is less than 2, not only the amount of impurities adsorbed but also the amount of scandium adsorbed decreases. For this reason, it is not preferable to allow a solution in an extremely low pH range to pass through the resin to be adsorbed.

[Aluminum removal step S42]
In the aluminum removal step S42, 0.1 N or less sulfuric acid is brought into contact with the chelate resin having adsorbed scandium in the adsorption step S41, and the aluminum adsorbed on the chelate resin is removed in the adsorption step S41.

When removing aluminum, the pH is preferably maintained in the range of 1 to 2.5, more preferably in the range of 1.5 to 2.0. If the pH is less than 1, not only aluminum but also scandium is removed from the chelate resin, which is not preferable. A pH exceeding 2.5 is not preferable because aluminum is not properly removed from the chelate resin.

[Scandium elution step S43]
In the scandium elution step S43, sulfuric acid of 0.3N or more and less than 3N is brought into contact with the chelate resin that has undergone the aluminum removal step S42 to obtain a scandium eluent.

When obtaining the scandium eluent, the normality of sulfuric acid used in the eluent is preferably maintained in the range of 0.3N or more and less than 3N, and more preferably maintained in the range of 0.5N or more and less than 2N. When the normality is 3N or more, not only scandium but also chromium is contained in the scandium eluent, which is not preferable. When the normality is less than 0.3 N, scandium is not appropriately removed from the chelate resin, which is not preferable.

[Chromium removal step S44]
In the chromium removal step S44, 3N or more sulfuric acid is brought into contact with the chelate resin that has undergone the scandium elution step S43, and the chromium adsorbed on the chelate resin in the adsorption step S41 is removed.

When removing the chromium, if the normality of the sulfuric acid used for the eluent is less than 3N, it is not preferable because chromium is not properly removed from the chelate resin.

[Iron removal process]
Moreover, although not shown in figure, iron may be contained as an impurity in nickel oxide ore. In this case, prior to the aluminum removal step S42, the chelate resin that has adsorbed scandium in the adsorption step S41 is contacted with sulfuric acid having a normality smaller than that of the sulfuric acid used in the aluminum removal step S42, and the chelate resin in the adsorption step S41. It is preferable to remove the iron adsorbed on the surface.

When removing iron, it is preferable to maintain the pH in the range of 1 to 3. If the pH is less than 1, not only iron but also scandium is removed from the chelate resin, which is not preferable. If the pH exceeds 3, iron is not appropriately removed from the chelate resin, which is not preferable.

<Re-adsorption of scandium eluent on chelate resin>
Although not an essential aspect, a neutralizing agent is added to the scandium eluate obtained in the scandium elution step S43 to adjust the pH to a range of 2 to 4, preferably 2.7 to 3.3 centered on pH 3. (Step S101), then a reducing agent is added (step S102), and then sulfuric acid is added to adjust the pH to a range of 1 to 2.5, preferably 1.7 to 2 centering on pH 2. .3 is adjusted (step S103) to obtain a solution after the pH adjustment of the scandium eluent, and the adsorption step S41, the aluminum removal step S42 and the scandium elution step S43 are performed again using the solution after the pH adjustment. Preferably it is done. By passing through these steps, the quality of the recovered scandium can be further enhanced. In addition, it is possible to reduce the chemical cost and the equipment scale when separating scandium from the scandium eluent.

The addition of the reducing agent is preferably carried out so that the oxidation-reduction potential (ORP) is maintained in a range in which the silver / silver chloride electrode is used as a reference electrode and exceeds 200 mV to 300 mV or less. When the oxidation-reduction potential is 200 mV or less, the sulfur content derived from the added sulfiding agent is precipitated as a fine solid, and the filter cloth is clogged in the filtration step after sulfidation, so that solid-liquid separation is deteriorated and productivity is increased. When the liquid is re-passed through the chelate resin, clogging or uneven liquid flow may occur in the resin tower, and uniform liquid flow cannot be performed. On the other hand, when the oxidation-reduction potential exceeds 300 mV, problems such as remaining iron ions adsorbing to the resin and inhibiting the adsorption of scandium may occur.

As the neutralizing agent, a conventionally known neutralizing agent is sufficient, and examples thereof include calcium carbonate. The reducing agent may be a conventionally known reducing agent, and examples thereof include a sulfurizing agent such as hydrogen sulfide gas and sodium sulfide, sulfur dioxide gas, hydrazine, and metallic iron.

When re-adsorbing the scandium eluent to the chelate resin, the chelate resin that has been used may be reused or a new chelate resin may be used, but from the viewpoint of preventing contamination of impurities. Therefore, it is preferable to reuse the chelate resin that has undergone the chromium removal step S44 or use a new chelate resin. In particular, by reusing the chelate resin that has undergone the chromium removal step S44, not only contamination of impurities can be prevented, but also the amount of chelate resin used can be suppressed.

<Purification of scandium eluent>
By performing the scandium elution step S43 again on the scandium eluent obtained in the scandium elution step S43, the concentration of the scandium eluent can be increased.

The more the scandium elution step S43 is repeated, the higher the concentration of the recovered scandium. However, even if the scandium elution step S43 is repeated too many times, the increase in the concentration of the recovered scandium is reduced. The number of repetitions is preferably 8 times or less.

<Concentration step S5>
Further, although not essential, a concentration step S5 is provided after the ion exchange step S4 to cause precipitation of scandium contained in the scandium eluent to separate it from impurities, and this precipitation is further treated with sulfuric acid and / or hydrochloric acid. It is preferable to perform the process which melt | dissolves and uses for the extraction start liquid used for solvent extraction of the following process.

As a specific concentration method, any of performing neutralization with hydroxylation, oxidation with oxidization, or both with neutralization with hydroxylation and oxidation with sulfoxidation may be employed, but it dissolves in the vicinity of the solubility of the obtained precipitate. It is preferable. By dissolving near the solubility of the obtained precipitate, the solid can be precipitated once and redissolved to an arbitrary concentration, so the scandium concentration can be arbitrarily selected and increased, and the liquid in the solvent extraction step of the next step This is an industrially very preferable aspect in that the amount and thus the equipment scale can be reduced.

The acid used for the precipitate obtained in this step may be either hydrochloric acid or sulfuric acid, but sulfuric acid is preferred.

[Hydrogen neutralization]
Below, the hydroxylation neutralization which is one aspect | mode of concentration is demonstrated. When employing hydroxyl neutralization, a neutralizing agent is added to the scandium eluent obtained in the ion exchange step S4 to obtain a precipitate, which is solid-liquid separated. Then, it is dissolved with an acid to obtain an acidic solution.

The neutralizing agent may be a conventionally known neutralizing agent, for example, calcium carbonate, slaked lime, sodium hydroxide, etc., but when the scandium eluent is a sulfuric acid solution, the neutralizing agent containing Ca content produces gypsum. Therefore, the neutralizing agent is preferably sodium hydroxide or the like.

The pH when the neutralizing agent is added is preferably 8 or more and 9 or less. A pH of less than 8 is not preferable because neutralization is insufficient and Sc may not be sufficiently recovered. When pH exceeds 9, since the usage-amount of a neutralizing agent increases, it is unpreferable at the point which becomes cost increase.

[Oxidation]
Then, the oxidation which is another aspect of concentration will be described. When employing oxalic oxidation, oxalic acid is added to the scandium eluent to form scandium oxalate crystals. At this time, the pH is preferably 0 or more and 0.5 or less. If the pH is too low, the solubility of scandium oxalate increases and the scandium recovery rate decreases, which is not preferable. If the pH is too high, impurities contained in the solution are precipitated and the scandium purity is lowered, which is not preferable.

Further, the amount of oxalic acid added is preferably 1.05 times or more and 1.2 times or less the equivalent amount required to precipitate scandium as oxalate. If the amount added is less than 1.05 times the required equivalent, there is a possibility that the entire amount of scandium cannot be recovered, which is not preferable. On the other hand, if the addition amount exceeds 1.2 times the required equivalent, the solubility of scandium oxalate increases, so that scandium is redissolved and the recovery rate is lowered, which is not preferable.

[Combination of hydroxylation neutralization and oxidation with oxalate]
Further, as another aspect of concentration, it is possible to carry out both the above-described neutralization with hydroxylation and oxalic oxidation. First, the scandium eluate obtained in the scandium elution step S43 is neutralized with the above-described hydroxide to obtain a precipitate containing scandium hydroxide. Next, hydrochloric acid is added to the precipitate to redissolve it, and oxalic acid is added to the redissolved solution to precipitate as scandium oxalate crystals. Next, the crystals are acid-dissolved as described above and subjected to the solvent extraction step S6.

By providing the concentration step S5, impurities contained in the scandium eluent can be largely removed, and the man-hours related to the ion exchange step S4 and the solvent extraction step S6 can be reduced. In addition, since the concentration of the starting solution to be subjected to solvent extraction can be arbitrarily adjusted, it is possible to reduce the capital investment by reducing the equipment scale in the solvent extraction step S6 and to stabilize the operation by stabilizing the starting solution concentration. Also have.

<Solvent extraction step S6>
In the solvent extraction step S6, the back extract is obtained by bringing the scandium eluent into contact with the extractant and adding the back extractant to the extract. Although the aspect of solvent extraction process S6 is not specifically limited, Extraction process S61 which mixes the extractant which is a scandium eluent and the organic solvent, and isolate | separates into the organic solvent after extraction which extracted scandium, and this extraction liquid, and this extraction After scrubbing step S62, in which a hydrochloric acid solution or a sulfuric acid solution is mixed with the organic solvent after the extraction and impurities are separated from the organic solvent to obtain the organic solvent after the washing, a back extractant is added to the organic solvent after the washing, and the organic after the washing It is preferable to include a back extraction step S63 in which scandium is back-extracted from the solvent to obtain a back extract. By performing the solvent extraction step S6, the purity of scandium contained in the scandium eluent can be further increased.

[Extraction step S61]
In the extraction step, scandium eluent and an organic solvent containing an extractant are mixed to selectively extract scandium into the organic solvent. There are various types of extractants, but due to selectivity with scandium, acidic extractants containing phosphorus, specifically di-2-ethylhexyl phosphate (D2EHPA), 2-ethylhexyl sulfonate-mono-2 -Ethylhexyl (2-ethylhexyl phosphoric acid) (trade name: PC-88A) or the like is preferably used.

During extraction, for example, it is preferably diluted with a hydrocarbon-based organic solvent. The concentration of D2EHPA or PC-88A in the organic solvent is not particularly limited, but it is preferably 10% by volume or more and 30% by volume or less, particularly 20% by volume in consideration of phase separation during extraction and back extraction. It is more preferable that it is 15 volume% or more and 25 volume% or less which becomes around%.

Further, the volume ratio of the organic solvent and the scandium eluent during extraction is preferably such that the molar amount of the organic solvent is 0.4 to 1.0 times the molar amount of metal in the scandium solution.

[Scrubbing (cleaning) step S62]
Although not an essential aspect, when an impurity element other than scandium coexists in the solvent from which scandium is extracted, the organic solvent (organic phase) is subjected to a scrubbing (washing) treatment before back extraction of the extract, It is preferable to separate the impurity element into the aqueous phase and remove it from the extractant.

As the solution (cleaning solution) used for scrubbing, a hydrochloric acid solution or a sulfuric acid solution can be used. When using a hydrochloric acid solution, a concentration range of 5.0 mol / l to 7.0 mol / l is preferable, and when using a sulfuric acid solution, a concentration of 2.5 mol / l to 3.5 mol / l in the case of D2EHPA. When using PC-88A, the concentration range is preferably 2.0 mol / l or more and 5.0 mol / l or less.

As the number of washing steps (number of times), when the phase ratio O / A = 1 of the organic phase (O) and the aqueous phase (A) is 1, it depends on the type and concentration of the impurity element. As an example, almost all elements can be separated to below the lower limit of analysis if there are 3 to 5 stages for DE2HPA and 3 to 8 stages for PC-88A.

[Back extraction step S63]
In the back extraction step S63, scandium is back extracted from the organic solvent from which scandium has been extracted. The back extraction step S63 is a step in which an organic solvent and a back extraction solution (back extraction start solution) are mixed to advance a back reaction during extraction.

In the present invention, since an acidic extractant is used as the extractant, in order to separate scandium from the organic solvent, it is necessary to break the bond of scandium contained in the organic solvent using an alkali. Therefore, the back extraction solution (back extraction start solution) is preferably a strong alkali solution including sodium hydroxide. When the back extraction solution is sodium hydroxide, scandium hydroxide is formed as a precipitate when the pH is 8 or higher. Therefore, considering both the generation of precipitate and the suppression of excessive use, scandium hydroxide The amount used is preferably such that the pH can be maintained between 8 and 9. And it is preferable that the density | concentration of sodium hydroxide is 5 mol / l or more and 8 mol / l or less.

When back-extracted with alkali, the product is a mixture of a solid scandium hydroxide and a liquid phase containing an organic solvent and an alkaline back-extracted solution, and is in the form of a slurry. Therefore, the product is first filtered to separate the scandium hydroxide solid from the liquid phase. Subsequently, an acid is added to the liquid phase, and the liquid phase is subjected to specific gravity separation into an organic phase and an aqueous phase. The scandium hydroxide solid obtained through these steps is supplied to the next step as a back extract. When the organic phase adheres to the scandium hydroxide solid, it is preferable to wash the solid.

<Recovery of scandium>
After the solvent extraction step S6, the scandium oxide can be recovered from the nickel oxide ore by performing the roasting step S8 of roasting the solid scandium salt. As described above, in the present invention, a scandium hydroxide precipitate has already been obtained in the back extraction step S63. Therefore, in the roasting step S8, solid scandium hydroxide can be baked as it is to obtain a scandium oxide solid. However, since this scandium hydroxide can still contain impurities, in order to increase the purity of scandium, before the baking step S8, the scandium hydroxide is acid-dissolved with hydrochloric acid or the like and oxalic acid is added to It is preferable to obtain scandium oxide by performing scandium precipitation step S7 to convert to scandium acid, and then subjecting scandium oxalate to roasting step S8.

[Scandium precipitation step S7]
The scandium precipitation step S7 is a step of neutralizing the back extract obtained in the solvent extraction step S6 with an acid, and further adding oxalic acid to precipitate and precipitate as a scandium oxalate solid to separate. The pH when dissolved in the acid is preferably 0 or more and 0.5 or less. If the pH is too low such as less than 0, the solubility of scandium oxalate increases and the scandium recovery rate decreases, which is not preferable. If the pH exceeds 0.5, impurities contained in the solution are precipitated and the scandium purity is lowered, which is not preferable.

The amount of oxalic acid added is preferably 1.05 times or more and 1.2 times or less the equivalent amount required to precipitate scandium as oxalate. If it is less than 1.05 times, there is a possibility that the entire amount of scandium cannot be recovered, which is not preferable. On the other hand, when added in excess of 1.2 times, the solubility of scandium oxalate increases, so scandium is redissolved and the recovery rate decreases, or excessive oxalic acid is decomposed to reduce the excess oxalic acid. This is not preferable because the amount of the oxidizing agent used increases.

[Roasting step S8]
The roasting step S8 is a step in which the precipitate obtained in the scandium precipitation step S7 is washed with water, dried, and roasted. By going through the roasting step S8, extremely high-quality scandium oxide can be obtained.

The baking conditions are not particularly limited. For example, the baking may be performed in a tubular furnace and heated at about 900 ° C. for about 2 hours. Industrially, it is preferable to use a continuous furnace such as a rotary kiln because drying and baking (roasting) can be performed in the same apparatus.

Hereinafter, the present invention will be described in more detail by way of examples, but the present invention is not limited to these descriptions.

<Example 1>
[Leaching step S1]
First, nickel oxide ore is charged into an autoclave together with concentrated sulfuric acid, and a slurry containing valuable metals such as scandium and nickel is produced over 1 hour under conditions of 245 ° C., and various valuable metals are contained from this slurry. Solid-liquid separation into leachate and leach residue was performed.

[Neutralization step S2]
And calcium carbonate was added to this leachate, and the neutralized starch and the liquid after neutralization were obtained. Valuable metals such as scandium and nickel are contained in the solution after neutralization, and most of impurities such as aluminum are contained in the neutralized starch.

[Sulfurization step S3]
Subsequently, hydrogen sulfide gas was blown into the liquid after neutralization, and nickel, cobalt, and zinc were separated from the liquid after sulfidation as sulfides.

[Ion exchange step S4]
[Adsorption process S41]
Slaked lime was added as a neutralizing agent to this post-sulfurized solution to adjust the pH to 1.6. In addition, in order to clarify the behavior of elements that are not included in the liquid after addition of slaked lime, or even if included, the contents of the elements are very small. An adsorbent liquid having the composition shown in 1 was obtained.

Figure JPOXMLDOC01-appb-T000001

Subsequently, the adsorption source solution having the composition shown in Table 1 was passed through a column packed with a chelate resin (product name: Diaion CR11, manufactured by Mitsubishi Chemical Corporation) having iminodiacetic acid as a functional group. In addition, the resin amount of the column was 40 liters, and the flow rate was 5.3 ml / min so that the SV was 8, and the flow rate was 2400 liters (Bed Volume: BV = 60). The liquid temperature at the time of liquid supply was 60 ° C.

[Aluminum removal step S42]
Next, 800 liters of a sulfuric acid solution having a concentration of 0.1 N was passed through the chelate resin at a flow rate of 27 liters per minute (SV becomes 40). The remaining aluminum-rich cleaning solution discharged from the column was stored as an aluminum cleaning solution, a part of which was sampled and analyzed by ICP.
The analysis values were Ni: 7 mg / l, Mg: 1 mg / l, Mn: 4 mg / l, Fe: 1 mg / l, Al: 84 mg / l, Sc: 3 mg / l. The analytical values of Cr and Ca were below the lower limit that can be measured.

[Scandium elution step S43]
Thereafter, 400 liters of a sulfuric acid solution having a concentration of 1 N was passed through the chelate resin (SV was 40) at a flow rate of 80 liters per minute. The eluent discharged from the column was stored as a scandium eluent, sampled and analyzed. The results are shown in Table 2. The analysis values of Mn and Ca were below the measurable lower limit.

Figure JPOXMLDOC01-appb-T000002

[Chromium removal step S44]
Subsequently, 80 liters of sulfuric acid solution having a concentration of 3N was passed through the chelate resin at a flow rate of 2.6 liters per minute (SV becomes 40). The cleaning liquid discharged from the column was stored as a chromium cleaning liquid, sampled and analyzed. The analytical values were Fe: 2 mg / l, Cr: 30 mg / l. Analytical values of Ni, Mg, Mn, Al, Ca, and Sc were below the lower limit that can be measured.

[Concentration step S5]
Next, sodium hydroxide was added to the scandium eluent having the composition shown in Table 2 to maintain the pH at 8-9, thereby forming a precipitate. The precipitate was dissolved by adding sulfuric acid to obtain a chelate eluent hydroxide solution. Table 3 shows the result of analyzing the composition of the chelate eluent hydroxide solution. The analytical values of Mg, Cr, Mn, and Ca were below the measurable lower limit.

Figure JPOXMLDOC01-appb-T000003

[Solvent extraction step S6]
[Extraction step S61]
103 liters of the solution having the composition shown in Table 3 was used as the extraction starting solution. This was mixed with 2.6 liters of an organic solvent prepared by adjusting the acid extractant, di-2-ethylhexyl phosphoric acid (D2EHPA, manufactured by LANXESS) to 13% by volume using the solvent Tclean N20 (manufactured by JX Nippon Mining & Metals). Then, the mixture was stirred at room temperature for 60 minutes to obtain an extracted organic phase containing scandium. No clad was formed during extraction, and phase separation after standing proceeded rapidly.

The composition of various elements contained in the extracted organic phase was analyzed. The value obtained by dividing the amount of each element contained in the extracted organic phase by the amount of each element contained in the original solution before extraction is taken as the extraction rate, and the results are shown in Table 4.

Figure JPOXMLDOC01-appb-T000004

From Table 4, it can be seen that scandium contained in the original solution before extraction is extracted into the extracted organic phase through the extraction step S61. In addition, it can be seen that the extracted organic phase contains almost no elements such as aluminum, nickel, magnesium, chromium, manganese, calcium, cobalt, copper, and zinc.

[Scrubbing (cleaning) step S62]
Next, a hydrochloric acid solution having a concentration of 6.5 mol / l is added to 2.6 liters of an organic solvent (extracted organic phase) containing scandium obtained in the extraction step so that the phase ratio (O / A) is 1. 2.6 liters were mixed and washed by stirring for 10 minutes. Thereafter, the aqueous phase was separated by standing, and the organic phase was again mixed with 2.6 liters of a fresh hydrochloric acid solution having a concentration of 6.5 mol / l and washed, and the aqueous phase was separated in the same manner. Such washing operation was repeated 3 times in total.

By washing the extracted organic phase three times, the impurity metal concentration other than the eluted scandium could be removed to a level of 1 mg / l or less. On the other hand, scandium remained at a low level of 10 mg / l, and it was found that only the impurities could be removed effectively without separating scandium extracted into the organic solvent into the aqueous phase.

[Back extraction step S63]
Next, sodium hydroxide having a concentration of 6 mol / l is mixed with the extracted organic phase after washing so as to have a phase ratio of O / A = 1/1 and stirred for 20 minutes, so that scandium is reversed to the aqueous phase. Extracted. Since it became the slurry state which the solid and liquid phase which precipitated by back extraction operation were mixed, it filtered and isolate | separated the solid and the liquid phase. The solid was washed with water to remove the organic phase adhering to the solid and the liquid after back extraction. For the liquid phase, hydrochloric acid was added to the liquid phase, stirred for 5 minutes, and allowed to stand to separate the organic phase of the organic solvent after back extraction and the aqueous phase of the liquid after back extraction.

Moreover, the composition of various elements contained in the solid (scandium hydroxide) deposited by the back extraction operation was analyzed. A value obtained by dividing the amount of various elements contained in the solid (scandium hydroxide) by the amount of various elements extracted in the organic phase in the extraction step S61 is defined as a recovery rate, and Table 5 shows the results.

Figure JPOXMLDOC01-appb-T000005

From Table 5, it can be seen that scandium contained in the original liquid before extraction can be almost completely recovered as a solid (scandium hydroxide) through the solvent extraction step S6. In addition, the recovered scandium hydroxide contains almost no elements such as aluminum, nickel, magnesium, chromium, manganese, calcium, cobalt, copper, zinc, and the quality of scandium contained in scandium hydroxide is It can be said that it is expensive.

[Scandium precipitation step S7]
Next, hydrochloric acid is added to the scandium hydroxide solid obtained above to maintain the pH of the slurry in the range of 1.0 to 1.5, while stirring to completely dissolve the scandium hydroxide solid. A redissolved solution was obtained. Next, in the redissolved solution, crystals of oxalic acid dihydrate (Mitsubishi Gas Co., Ltd.), which is twice the calculated amount of scandium contained in the redissolved solution, are dissolved and mixed with stirring for 60 minutes. This produced a white crystalline precipitate of scandium oxalate.

[Roasting step S8]
The scandium oxalate obtained in the above scandium precipitation step was suction filtered, washed with pure water, and dried at 105 ° C. for 8 hours. Subsequently, scandium oxalate was placed in a tube furnace and maintained at 850 to 900 ° C. and baked (baked) to obtain scandium oxide.

The scandium oxide was analyzed by emission spectroscopy. Table 6 shows the removal rate. Impurities other than scandium, particularly aluminum, nickel, uranium, and copper, can be almost completely removed, and the purity as scandium oxide Sc 2 O 3 is extremely high exceeding 99.9%. Pure scandium oxide could be obtained.

Figure JPOXMLDOC01-appb-T000006

<Example 2>
The same nickel oxide ore as in Example 1 was leached in the same manner as in Example 1, neutralized, and sulfidized to obtain a post-sulfurized solution having the composition shown in Table 7.

Figure JPOXMLDOC01-appb-T000007
(Unit is mg / l)

The ion exchange step and the concentration step were performed on the post-sulfurized solution in the same manner as in Example 1, and the obtained scandium hydroxide was dissolved again with sulfuric acid to obtain a chelate eluent hydroxide solution. Table 8 shows the results of analyzing the composition of the chelate eluent hydroxide solution.

Figure JPOXMLDOC01-appb-T000008

A chelate eluent hydroxide solution having the composition shown in Table 8 was used as an extraction starting solution, and subjected to solvent extraction using an acidic extractant. PC-88A (manufactured by Daihachi Chemical Co., Ltd.) was used as the acidic extractant, and this was diluted to 20% with the solvent Teclean N20 (manufactured by JX Nippon Mining & Metals). The extraction equilibrium pH was set to 0, and based on the ratio of the organic amount to the metal amount in the liquid, the organic amount (O) and the amount of the extraction start liquid (A) were selected as the conditions shown in Table 9.

Figure JPOXMLDOC01-appb-T000009

FIG. 2 shows the extraction rates of Sc, Th, U, Al and Fe contained in the organic solvent. From FIG. 2, when the organic amount / metal amount (unit: mol / mol, the same applies hereinafter), which is the ratio of the organic amount to the metal amount, is in the range of 0.4 to 1.0, scandium is replaced with thorium, aluminum or iron. As a result, scandium can be concentrated in an organic solvent. Specifically, when O / A is 2.00, the extraction rate of thorium is 0%, the extraction rate of iron is 4%, and the extraction rate of aluminum is 6%, whereas the extraction rate of scandium Is 63%.

On the other hand, if the organic amount / metal amount is less than 0.4 times, the phase separation between the organic phase and the aqueous phase is poor, which is not preferable. Further, when the amount of organic / metal exceeds 1.0 times, metals other than scandium may be contained in the organic phase, which is not preferable.

Subsequently, sulfuric acid was mixed with the organic solvent PC-88A after extraction of the metal according to Example 2-2, and washed under the conditions shown in Table 10.

Figure JPOXMLDOC01-appb-T000010

FIG. 3 shows the relationship between the sulfuric acid concentration and the cleaning rate. The washing rate is a ratio of a metal separated from an organic solvent and contained in sulfuric acid. In any sample, uranium can be separated from the organic solvent and removed. In particular, when the sulfuric acid concentration is 2 mol / l or more and 5 mol / l or less, 80% or more of uranium is separated from the organic solvent. Can be removed.

Subsequently, sodium hydroxide or sodium carbonate was mixed in an organic solvent containing scandium and back-extracted. Table 8 shows the results of analyzing the composition of the back extract after back extraction. The recovery rate was the ratio of the weight (unit: mg) of each component contained in the solution after back extraction to the weight (unit: mg) of each component contained in the organic phase after washing with sulfuric acid.

Figure JPOXMLDOC01-appb-T000011

From Table 11, it was confirmed that scandium can be recovered at a recovery rate of 95% or more.

S1 Leaching process S2 Neutralization process S3 Sulfurization process S4 Ion exchange process S5 Concentration process S6 Solvent extraction process S7 Scandium precipitation process S8 Roasting process

Claims (12)

  1. A leaching step of charging nickel oxide ore containing scandium, aluminum and chromium into a pressure vessel together with sulfuric acid, and solid-liquid separation into a leaching solution and a leaching residue under high temperature and pressure;
    A neutralizing step of adding a neutralizing agent to the leachate to obtain a neutralized starch and a post-neutralized solution;
    A sulfiding step of adding a sulfiding agent to the post-neutralization liquid and separating the nickel sulfide and the post-sulfurization liquid;
    An ion exchange step of contacting the post-sulfurized solution with a chelate resin to adsorb the scandium to the chelate resin, and obtaining a scandium eluent;
    A solvent extraction step of bringing the scandium eluent into contact with an extractant and adding a back extractant to the extract to obtain a back extract;
    A method for recovering scandium, comprising baking the back extract to obtain scandium oxide.
  2. The chelate resin is a resin having iminodiacetic acid as a functional group,
    The ion exchange step includes
    An adsorption step of contacting the post-sulfurized solution with the chelate resin to adsorb the scandium to the chelate resin;
    An aluminum removing step of contacting sulfuric acid of 0.1 N or less with the chelate resin adsorbing scandium in the adsorption step, and removing the aluminum adsorbed on the chelate resin in the adsorption step;
    A scandium elution step of contacting the chelate resin having undergone the aluminum removal step with sulfuric acid of 0.3N or more and less than 3N to obtain the scandium eluent;
    2. The scandium recovery method according to claim 1, further comprising a chromium removal step of bringing 3N or more sulfuric acid into contact with the chelate resin that has undergone the scandium elution step and removing chromium adsorbed on the chelate resin in the adsorption step.
  3. After the ion exchange step, the method further comprises a step of producing a scandium-containing starch from the scandium eluent, and acid-dissolving the starch to obtain a scandium concentrate.
    The scandium recovery method according to claim 1 or 2, wherein the solvent extraction step includes a step of bringing the scandium concentrate into contact with the extractant to obtain a back extract.
  4. The concentration step includes
    A step of generating a neutralized product by adding a neutralizing agent to the scandium eluent and adjusting the pH to a range of 8 to 9;
    The scandium recovery method of Claim 3 including the process of acid-dissolving the said neutralized material with a sulfuric acid or hydrochloric acid.
  5. The concentration step includes
    Adding oxalic acid to the scandium eluent to produce scandium oxalate crystals;
    The method for recovering scandium according to claim 3, comprising a step of acid-dissolving the scandium oxalate crystals with sulfuric acid or hydrochloric acid.
  6. The scandium recovery method according to any one of claims 1 to 5, wherein the extractant is an acidic extractant.
  7. The method for recovering scandium according to claim 6, wherein the acidic extractant is di-2-ethylhexyl phosphoric acid.
  8. The back extractant is sodium hydroxide having a concentration of 5 mol / l or more and 8 mol / l or less,
    The scandium recovery method according to claim 1, wherein the back extract is a precipitate of scandium hydroxide.
  9. The solvent extraction step includes
    An extraction step of mixing the scandium eluent and the extractant, which is an organic solvent, and separating the organic solvent and the extraction residual liquid after extraction by extracting scandium;
    After the extraction, the organic solvent after the extraction is mixed with a hydrochloric acid solution having a concentration of 5.0 mol / l to 7.0 mol / l or a sulfuric acid solution having a concentration of 2.5 mol / l to 3.5 mol / l. A scrubbing step for separating the impurities from the organic solvent and obtaining the organic solvent after washing;
    A back extraction step of adding the back extractant to the washed organic solvent and back extracting scandium from the washed organic solvent to obtain the back extract. Scandium recovery method.
  10. The scandium recovery method according to claim 6, wherein the acidic extractant is 2-ethylhexylsulfonic acid-mono-2-ethylhexyl.
  11. The solvent extraction step includes
    An extraction step of mixing the scandium eluent and the extractant, which is an organic solvent, and separating the organic solvent and the extraction residual liquid after extraction by extracting scandium;
    After the extraction, the organic solvent after the extraction is mixed with a hydrochloric acid solution having a concentration of 5.0 mol / l to 7.0 mol / l or a sulfuric acid solution having a concentration of 2.0 mol / l to 5.0 mol / l. A scrubbing step for separating the impurities from the organic solvent and obtaining the organic solvent after washing;
    Adding 5.0 mol / l or more and 8.0 mol / l or less of sodium hydroxide to the organic solvent after scrubbing obtained in the scrubbing step to obtain a scandium hydroxide starch;
    The method for recovering scandium according to claim 10, further comprising: adding an acid to the scandium hydroxide starch to obtain a scandium solution.
  12. After the solvent extraction step, further comprising a scandium precipitation step of dissolving the back extract with hydrochloric acid and adding oxalic acid to the hydrochloric acid solution obtained by this dissolution to obtain scandium oxalate crystals,
    The scandium recovery method according to any one of claims 1 to 11, wherein the roasting step includes a step of firing the crystals of scandium oxalate.
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